Industrial process using a forced-exhaust metal furnace and mechanisms developed for simultaneously producing coal, fuel gas, pyroligneous extract and tar

ABSTRACT

This patent of invention is related to a process and a furnace developed for production of charcoal with recovery of gases, tar and pyroligneous extract. The unity system is composed by a metallic furnace, a loading platform, a carbonization platform and unloading platform. For continuous generation of gases, the process operates with multiple carbonization platforms and one or more furnaces for carbonization platform. The furnace is provided with air inputs in strategic side points and mechanism for relieving pressure. The carbonization system is composed by an exhauster, special pipes for conducting the gases, and devices for the recovery of condensable. The gases generated in the process are directed to a burner, a gasifier or directly in a boiler to generate thermal and/or electrical energy. The technology presents, exclusively, a gravimetric yield in fuel gas superior to 60% and a productivity on charcoal above 800 kg/h, so that each operating cycle of the furnace takes less than 5 hours. The coal is discharged hot, after carbonization and loaded on wooden billets immediately after unloading. The process combines technical, economic, operational, and environmentally viable solutions.

FIELD USE

This patent relates to a process and a furnace designed for charcoalproduction with the recovery of the gases, tar and pyroligneous extract.

PRIOR ART

This invention relates to a process and a furnace for industrialproduction of charcoal and recovery of the gases generated in theprocess, in order to solve the problem inherent to carbonization processas implemented today by most charcoal. In Brazil, most of the charcoalproduction, around 70% comes from the traditional charcoal kilns ofbrick kilns, said “rabo-quente furnace.” These furnaces have a lowpercentage yield by weight in the conversion of biomass into charcoaland have high long production cycles. Typically they are spending fivedays to carbonize biomass and 7 days to complete cooling, i.e. betweenthe loading and unloading are used about 12 to 14 days.

In the traditional process for producing coal in brick kilns type“Rabo-quente “, wood and coal are respectively loaded and unloadedmanually, subjecting the furnace operator to severe and harsh workingconditions. The process control means are highly subjective anddependent on the experience of the operator who must evaluate as sensorycriteria, parameters such as the color of the smoke to determine theclosing of the openings in the furnace wall. These openings, donemanually, are called “baianas” in the furnace surface and “tatus” in thefurnace base. In addition, generated gases in the carbonization processare released into the atmosphere without any control and/or use,resulting in a significant energy waste. The released gases by thesefurnaces still harm the operators working environment, as the smokereleased when in contact with eyes and mucous membranes cause irritationand may also contain toxic substances. Added to the problems reportedhere, there is still the question of the large-scale production to meetthe major consumers of charcoal, efficiently, automated, mechanized atlow cost and without damaging the environment.

Since 2001, we presented to INPI a series of patent grant requestscontaining proposals for the solution of these problems. These requestsrelated to the object of this report are discussed and presented inchronological order below.

On Oct. 2, 2001, it was filed with the INPI under the number PI0104858-9 the request for the grant of a patent relating to a Containerfurnace for the production of charcoal. In this application, we sought ametallic furnace with forced exhaust gases, which must be placed in acombustion chamber inside an insulating well. In the combustion chamber,forestry waste or low grade firewood is burned to provide power to thecarbonization process. This invention has only one control valve to thewhole process, which is located below the combustion chamber of thefurnace. The gases from the process are sucked by a hood, burned andthen discarded to the environment. This system, although it has beenproposed to solve the problems mentioned above, such as shortercarbonization time and improve process control and improve workingconditions for workers, not completely cover all energy, environmentaland operational issues. For example, by this charging system must bedone manually. The cooling step takes place inside the furnace, whichreduces the uptime of each furnace. Furthermore, the system is equippedwith only one control valve, which for small volumes can be acceptable,but for industrial furnaces of large volume, such as on the proposal ofthis invention are not effective, being necessary the process control inseveral points of the furnace. Therefore, it is a project, evensurpassing the prior art of the carbonization process, does not presentat the time of its protocol all additional conditions required tocomplete solution of the energy, environmental and operational problems.These conditions and improvements were being presented in other patentapplications and processes required to INPI, from 2001, including thisnew patent application, which we require at the present time (2014).

On Dec. 29, 2005, it was filed with the INPI under the number PI0506224-1 the request for grant of a patent relating to a gasifiercoupled to a Container furnace. The document discloses the use of thecontainer Furnace as a gasifier through the combined input of steam andoxygen by means of gas distributors inside the furnace in which biomassgasification processes. PI 0506224-1 also discloses the use of fuelgases as an energy source for the drying process of wood; the use ofthermal insulation to increase the life of the furnace; and the presenceof a breast water to ensure the tightness of the furnace. This proposalor innovation claim is an improvement or enhancement in relation to the(PI 0104858-9) because it uses a combustion chamber below the furnacefor supplying power to the process; It uses forced extraction of gases;there is a cost effective method of sealing the furnace and the processtakes place in mobile metal furnaces. Although the PI 0506224-1 documentdeals with the Container furnace functionality as a gasifier, is notoffered a definitive solution to the production of large scale charcoal,since the charcoal yield in a carbonization furnace which operates as agasifier is low compared to the traditional process. This invention,filed in December 2005, aims to present and/or characterize theContainer furnace as a gasification equipment, associated with acarbonization system. However, it still does not present completesolutions for environmental mechanization, automation and optimization,energetics and operational, which will be demonstrated in thisapplication.

On Apr. 28, 2006, it was filed with the INPI under the number PI0603433-0 the request for grant of a patent relating to a continueproduction process of coal in Containers furnaces with use of fuel gasesfrom the carbonization of biomass. In this document is presented as maininnovation to prior applications, the concept of metal furnace providedwith orifices with control mechanical valves distributed to the side ofthe furnace. These valves can be opened or closed as required andcontinuation of carbonization. At the beginning of the process, thefurnace must be placed inside a masonry shirt under a combustionchamber, which provide the energy required for carbonization of biomass.This chamber may have one or more air inlets to assist the control.According to PI 0603433-0, the proposed invention presents a time ofcarbonization between 8 and 16 hours depending on the moisture contentof the wood. This time is significantly shorter than the carbonizationtime of a brick furnace, which is an average 5 days. For small and/orlow thickness biomass, such as antlers and grass, carbonization lastedbetween 3 and 4 hours. It is understood by a final carbonization, theproduction of charcoal, characterized by containing a fixed carboncontent between 70 and 85%. This application also reveals that the basiccycle consists of four steps: loading, carbonization, cooling andunloading. For each step is necessary a Container furnace to ensure thecontinuity of the cycle and to a greater production, it is necessary tomanufacture multiple furnaces in cyclic operation.

PI 0603433-0 presents innovation to the state of the art the presence ofair intake valves positioned over the lateral surface of the metalfurnace. This is an important solution, since it allows the operator acontrol of the air inlet by on/off closing/opening, gradual or full, sothat the inlet air flow can be monitored by equationing of the inputspeed, area and valve opening time. This is an evolution of the manualprocess to a mechanized and potentially automatable process. Thecontrolled form of air injection also allows an optimization of theenergy content of the gas generated in the carbonization, qualifying itas a potential fuel for use, for example, in generation of electricity.

However, on the need to keep coal inside the Container furnace duringthe cooling stage, the proposed invention in PI 0603433-0 makesimpossible the continued use of the furnace, only to coal production.Furthermore, the document does not disclose a proposal to solve therapid or instantaneous unloading the furnace.

Continuing with the same project on Aug. 11, 2006, it was filed withINPI under the number PI0603622-8 a patent grant request referring to acontinuous production process of charcoal in Containers furnaces, thistime considering the design with the exhaust gas system, which can occurat the bottom, top and/or side of the furnace. In this request, the mainimprovement over the previous process is the establishment of threeoptions to the exhaust point in the furnace, which may be effected bytop, bottom or side, alone or in combination. This innovation alsoconsists in a evolution or innovation of the prior art, since in anyprocess or carbonization technology does not occurs simultaneouslyexhaustion of gas in distributed form over the entire loading surface,which enhances productivity and yield, as it provides greater area andvolume in homogeneous conditions of fluid dynamics and heat transfer. Intraditional processes, it is conventionally the occurrence ofcarbonization front or line that runs through the load usually in asingle direction, especially in the vertical direction or along thelength of the logs. Obviously, coexists a carbonization front thatoccurs individually in each biomass part, of the external way (bark) tothe center or core of the log.

Also on Aug. 11, 2006, a second patent grant request was filed with INPIunder the number PI0603623-6 for a continuous production process ofcharcoal in Containers furnaces with ignition at top, bottom and sidesof the furnace. This is an improvement over the prior art, since theignition usually takes place solely by bottom and/or top of the furnace.Similarly to the application PI0603622-8, this solution intends toensure the use of this feature in an exclusive way.

However, in the course of development of this research, technically, theaddition of two or more exhaust points leads to the need for greatercontrol over the process due to different carbonization fronts formed.In addition, ignition points at different positions in height andcircumference of the furnace lead to unsafe operation because gasesgenerated by one of the carbonization fronts may come into contact withthe produced flame/coal by another front. Depending on the temperatureand hydrogen content, water vapor and oxygen in these areas, there is arisk of explosion. Given these possibilities/risks, improvementproposals in PI0603623-6 did not moved and did not result in real gains.In addition, this system does not propose a global solution, that makeit viable, technically, economically, environmentally and energeticallythe operation of an industrial plant for production of charcoal.

On Oct. 10, 2006, it was filed with the INPI under the numberPI0605093-0 a patent grant request concerning the Container furnace forsugarcane bagasse and/or biomass gasification. In this application it isdescribed a gasification process using the Container furnace. Similar toprevious texts is emphasized that this request does not propose asolution for coal unloading in order to release the furnace from coolingprocess, but reveals the use of spray nozzles to speed up the coolingprocess inside the furnace.

On Oct. 24, 2008, it was filed with the INPI under the numberPI0804554-2 a patent grant request relating to a process and automatedequipment of charcoal continuous production, with continuous monitoringof weight and temperature. In this request is described a method andequipment for charcoal production, comprising a metallic furnace withdistributed automatic valves on furnace surface, dividing the furnaceinto ‘n’ areas, according to the needs of each project. The furnace mayfurther be provided with an inner liner to distribute gases. The processis monitored via mechanisms for measuring temperature, pressure andweight and controlled via manual or automatic devices. Process Controlis assisted by a software that establishes a pattern curve or processmap and continuously informs the operator which points of the furnacecontrols and adjustments will be necessary. The production cycle of thisprocess involves four steps, requiring a furnace in each of them, toensure the continuity of the cycle. This document also discloses the useof the furnace itself to promote rapid cooling of the charcoal producedby spraying water inside the furnace or by cooling (in external heatexchanger) and gas recirculation in the furnace. PI0804554-2 alsoproposes that the furnace loading and unloading are done with the samebeing “tumbled”, i.e., in the horizontal direction. In summary, thepresented solution tries to solve the problems inherent to industrialprocess of charcoal production, but it fails when again it back usingthe furnace, dimensioned object and designed to withstand the hightemperatures, to promote cooling. Again this solution still does notshow a global innovation as the optimization and energetic efficiency,environmentally and operationally of the process for nullifying theexclusive use of the furnace for the carbonization process, for notpresenting detailed solutions of mechanization, automation and control.Another flaw presented in the process concerns the proposals for loadingand unloading the furnace. “Topple” the furnace, in other words, removeit from the vertical position and rotate it to landscape, results in acomplicated process, especially when working with large capacityfurnaces (up to 30 m3 of usable volume). The needed equipment to carryout these operations are costly, decharacterizing the industrialapplication of this type of loading/unloading for an industrial furnace.Another aspect to be considered refers to the sizing of the furnace,which should have structural reinforcements to meet the proposedcharging, resulting in an increase in design cost.

On Dec. 3, 1998, it was filed with the INPI by a third company under thenumber PI9806361-8 a patent grant request related to a process andfurnace for the destructive distillation of wood in order to obtaincharcoal and/or recovering volatile wood products, or obtaining the drywood. In this document, the reactor used to promote the carbonization oforganic matter has a cylindrical shape, which is positionedhorizontally. In this reactor, the wood is supported by rails, wherebypart of the gases produced during carbonization itself is returned toheat the pyrolysis bed of a second reactor. In the upper region of thereactor during the carbonization stage, the injected gas and theproduced gases are sucked and pass through a separator. A portion of thegas is then reheated in a heat exchanger to 280° C. to 450° C. andreinjected into the bed through the pyrolysis furnace grids. It istherefore an upward gas flow inside this vessel.

The remaining pyrolysis gases will go to a combustion chamber and theproducts of this reaction are brought to the reactor during the dryingstep of the wood. At the gas stream that is injected, are added thegases released during drying. Similarly to the pyrolysis reactor, thegas flow is upward.

The sucked gases from the drying chamber are then taken to a thirdreactor, in which it runs through the produced coal also upwardspromoting its cooling.

All drying, combustion and cooling processes occur simultaneously andtake an estimated time of 18 hours. The equipment related to combustiongases and heat exchanger are fixed, as well as reactors, which occurssimultaneously and consecutively the steps of pyrolysis, drying andcooling. For all the steps can occur in the same reactor, the ducts arealways exchanged and a tank assumes the following cyclic steps:pyrolysis—cooling—drying. That is, in this process, the reactor is fixedand the flow of gases is mobile; there is a reversal of the flow ofdrying, of the pyrolysis flow and of cooling flow between the reactorduring all the process.

The objective of this patent, PI9806361-8, filed by third parties, is topromote charring, drying and cooling simultaneously in differentcontainers, with alternating flow of gas generated and produced duringthe process, either by the reactors themselves/load or with the use ofexternal equipment such as heat exchangers.

The drying process described in PI 9806361-8 has some disadvantages.Most of them comes from the fact that there is many equipment, pipes andregisters to promote the turnover among containers/reactors. Thus, notonly the control strategy becomes more troublesome, but there is greatpotential for the occurrence of problems such as condensation,incrustation and obstruction because of the condensable gases arisingfrom coal production, such as tar and pyroligneous.

As in the same reactor simultaneously occurs pyrolysis, cooling anddrying, there is not possibility to build a tank that specifically meetseach of these steps. There are no construction details given in thepatent, but it would be ideal that the tank in pyrolysis was a thermalinsulator and that otherwise occur during cooling. This lay-out createsthe obligation for either property have to be prioritized in theconfiguration of a single device with multiple uses.

In the patent PI 9806361-8, it is mentioned that wood will not be burnedto start the carbonization process, but there is no mention of how itsstart-up will be given. One possibility would be a gasometer for gasesstorage that will be circulated, but due to the presence ofcondensables, this idea can not be as viable as simple combustion of aninitial amount of wood.

The processes shown in the present state of art, therefore, flaws intheir design and conception and they do not offer complete solutions tothe problem of industrial production of charcoal. All constructions usethe furnace for the production of charcoal as a container for promotingcoal cooling and there is not a solution comprising technical, economic,energetic and environmental viability simultaneously. This presentapplication intends to present this innovative solution, global, thatcovers and outperforms other filed applications, in particular for theenergy use of biomass, furnace operation, design, layout and operationallogistics including coal unloading in order to release the furnace fromcooling step, which increases effectively the process productivity;allowing the furnace to be used for its most noble and sole purpose:coal and fuel gas production.

Solution of the Problem

The industrial furnace for charcoal production consists of a metal,mobile container with cross section predominantly circular, whose aim isto convert biomass inserted inside in charcoal, in the shortest possibletime and with greater gravimetric yield (ratio between the mass ofcharcoal per mass of dry biomass). The proposed solution encompasses,besides the carbonization Container furnace, all other systemcomponents, which together enable this project to an energetically,operationally and environmentally production from biomass derivatives:bioredutor (charcoal), tar, pyrolignous liquor and combustible gases.

Thus, the project comprises a unique and differentiated system of gasesand vapors generated during the carbonization process. This systemcomprised by an exhauster generates the necessary depression inside thecontainer as well as a special fluid dynamics, which promotes both gasesexhaustion and the injection of atmospheric air. The effect of gasesexhaustion, together with the control mechanisms and ignition of theprocess allows to reduce the time required for the conversion of biomassinto charcoal from 8 to 12 hours (which constitutes the best resultsreferred to in the processes described in the prior art), for a timeless than 4 hours—this amount was established for a wooden mass put intothe furnace around 10 tons. This advance, specifically for productivity,was only possible due to furnace design improvement and supportstructures, layout of the plant, mechanization, automation and operationof process control techniques, which are described in this report in duecourse.

Masonry furnaces for the production of charcoal have as a major drawbackthe fact that their high time for converting biomass into charcoal, asmentioned above, between 12 and 14 days. This high time is partly due tobad distribution of gas flow inside the furnace.

The industrial furnace for the production of charcoal solves thisproblem by the introduction of holes at strategic points along theexternal surface of the furnace, so as to maintain the rate of isothermof 200° C. always high. This is achieved by the heat of the furnaceprofile analysis over time of carbonization and the subsequentintroduction of holes at the points of lower speed. The furnace, objectof this patent, had their points of slowness or deceleration of thefront of carbonization (which we call isotherm of 200° C.), mapped andminimized by adding holes to the atmospheric air inlet. The inlet air inthese specific points accelerates carbonization, since it promotes thecombustion of the combustible gas present in this region; whichultimately “pull” the carbonization line, which usually occurs from topto bottom in the vertical direction of the furnace.

No carbonization furnace either metallic or masonry, in operation todayand/or in remote dates has in its structure, this type of industrialcontrol input and the air flow, which can be manual or automated andstill restricted to the inlet air, enriched oxygen, or even a heatedinert gas. In traditional brick furnace, especially the “rabo quente”,these air inlets, called “baianas” and armadillos are manually operateda sensory and handmade way, with no possibility of an enhanced controlof input flow and monitoring of the speed of isotherm or carbonizationfront, that is not merely sensory, by touch and smell. Coupled with theabsence of proper control of temperature and oxygen supply, in the “raboquente” furnace there are presence of cracks and holes in the masonrywall that result in frequent explosions and collapse of the furnaces,with consequent financial loss.

The present invention provides as a solution to the problem of unwantedleakage of air and explosion in a sealed metal furnace with physicalisolation in all areas and bases which connect the furnace to the restof the structure and/or allow controlled air entrance. To ensure thisseal, valves for air inlet are mechanical and have the gasket seal.Likewise, the furnace base and the top cover for charging have sealingring with cooled flange. Moreover, the design/furnace presented as anindustrial solution in this invention has valves to pressure relief,appropriately designed and positioned over the structure and of thefurnace set coupled to the gas conduction pipe system. Such valvesoperate, whenever necessary, such as relief systems, opening andreturning to the original position without any dependence of humanactivity. This is an important advantage of the proposed furnace forindustrial production of charcoal compared to the remainingcarbonization furnaces because it allows to regulate pressure inside thefurnace.

Another advance of extreme importance to the state of art is thedevelopment of a mechanism that allows unloading of coal still hot fromcarbonization furnace in a second cooling container to, thus release thecontainer furnace to its more noble use: the exclusive production ofcharcoal.

For this, the Container Furnace has a bipartite discharge valve, locatedin the lower region of the furnace, whose function is to release to basethe charcoal produced without waiting for the cooling step. With theinclusion of the lower discharge valve the availability of the Containerfurnace for the productive process is increased considerably, reducingthe number of investment in furnaces. Although the vent valve is the keyelement for this inventive jump, the proposed solution consists of aseries of points, which together enable the unloading of coal, stillred-hot, safely and quickly. This design allows the furnace to bedesigned and manufactured with adequate thermal insulation, i.e., lightand efficient. The results of energy balance showed that in this way,the thermal losses of this furnace is less than 5% of all the energycontained in the firewood, this fuel with a moisture content of below30%. The second advantage derived from this invention is the design andfabrication of a container own for receiving coal still in carbonfixation step, i.e., above 400° C. It is a metallic cylinder, but withlow weight, below 4 tons, with no insulation and equipped with a uniquesystem of water sprinklers on the coal during the unloading. Thiscontrolled water spray system over the falling down coal does notinterfere with the mechanical properties thereof, since the amount ofwater does not exceed the volume required only for enthalpic energyremoval or vaporization thereof. And especially, the water spray reducesby more than 70% the time needed for coal cooling in the propercarbonization furnace without loss of their mechanical properties andalso without unintentional and uncontrolled maintenance of carbonfixation process that occurs in other prior art furnaces.

The furnace charging process was also optimized. Instead of loading thefurnace from the bottom, as described in the prior art, the presentinvention, object of this report proposes a loading system from theupper part of the furnace, eliminating the necessity to rotate, tilt ortip over the furnace for loading. This improvement over prior artconsiderably reduces the charging time of the furnaces, resulting inproductivity gain by increasing the availability of the furnace for thecarbonization process. Charging from the top also allows a betterhomogenization of the load and greater operational regularity.

This new technology has an exclusive and unique system of simultaneousmonitoring in real time of all process variables, as follows;

-   -   Content of firewood moisture    -   Mass of firewood put into the furnace    -   Gravimetric yield in coal    -   Content of pyroligneous in the collected gas.    -   Air intake flow    -   O₂ stoichiometric excess percentage in combustion reaction    -   Complete combustion percentage    -   Collected tar fraction, condensed and burned    -   Collected pyroligneous fraction, vaporized and burned    -   Temperature measurements (gas, insulation, furnace, housing,        coal)    -   Activation energy of the reaction    -   Pyrolysis Heat    -   Percentages of fuels derived from wood that provide energy to        the carbonization process    -   Exhaust Flow    -   Content of O₂, N₂, H₂, CH₄, CO₂, CO and CnHm of non-condensible        gas    -   % excess of stoichiometric air    -   % of complete combustion    -   % of burning coal    -   % burning tar    -   % burning pyroligneous    -   % burning CNG    -   % of the reaction between C and water vapor    -   % of complete combustion reaction of C with the formation of CO        and H2

The innovations proposed as a solution to these problems will bepresented in detail in the following items.

DESCRIPTION OF THE DRAWINGS

The foregoing aspects and many of the attendant advantages of thisinvention will become more readily appreciated as the same become betterunderstood by reference to the following detailed description, whentaken in conjunction with the accompanying drawings, wherein:

FIG. 1 shows sectional views of a furnace for the industrial productionof charcoal and the recovery of generated gases;

FIG. 2 shows cross-sectional views of the furnace of FIG. 1 illustratingthe opening and closing of the furnace during the loading and unloadingof the furnace;

FIG. 3 is a schematic view of the furnace shown in FIG. 1 including theequipment used for gas recovery; and

FIG. 4 is a cross-sectional view of the furnace illustrating theunloading of the furnace.

DESCRIPTION OF THE INVENTION

The metal container of the industrial furnace (1) for the production ofcharcoal has its inside volume divided virtually into three partsaccording to FIG. 1: Top (R1), core (R2) and lower frustum (R3). Thereare no physical barriers between regions; the division listed here isdone only to simplify the description of the various components of theproposed solution.

The top region (R1), located at the top of the furnace may be in coneshape or torresferic. This region may be partially divided or completelyseparated from the central cylinder, as shown in FIG. 2, assuming thecover function (2) to the biomass charging hole inside the furnace (3).Moreover, its truncated cone-shaped or torresferic shape allows thecreation of relief mechanisms to control the internal pressure of theprocess (4). This pressure relief mechanism is defined as a relief hole,preferably circular in the surface of the top region sealed by a mobilerelief cover, compatible with the hole that vertically moves upwardswhen the internal pressure rises beyond the expected and returns to theseat of the hole when regularized the internal pressure. The hole may bepositioned anywhere on the top surface of the region, but it shouldpreferably be concentric with the diameter close to the furnace. Therelief cap should have an area and weight compatible with the furnacewith the raw material and the process, which to this inventioncorresponds to an area ranging between 0.25 and 0.45 m2 and weightbetween 30 and 55 kg. The initial dimensioning of valves for burstrelief had a base on the standard NFPA68/2007, but due to limitedapplicability of this standard to the industrial furnace for charcoalproduction, the final values for area and weight was due to thedevelopment of own mathematical models associated to blast testsconducted in situ in the furnace. The seal (5) between the cover and therelief hole must be made by a material resistant to temperatures up to95° C., soft to absorb impacts and promote the sealing, since thepressure necessary to ensure sealing process will be function only ofcover weight. The mobile relief cap has its vertical travel limited by aseries of tabs, preferably three equidistant or hinged connecting thepressure relief hole cap (4) to the top region (R1).

In its optimal configuration, the top region has the largest diameter,in the case of frusto-conical shape equal to the diameter of the centralcylinder region, with a frustoconical inclination to the vertical musthave an angle (Al) between 8 and 25°. The region is internally insulatedwith ceramic fiber blanket (6) and this is isolated from contact withthe raw material inside the furnace by a thin plate (thickness 1.5 mm)of stainless steel (7). This plate also prevents contact of theinsulating blanket with vapors and tar dispersed in the internalatmosphere of the furnace. The top region (R1) is fixed to the centralcylinder region via specific mechanisms positioned near the largerdiameter top. These mechanisms are pivot pins (8) secured to the centralcylinder region which fit over guides (9) attached to the top region(R1). The joint is sealed using special seals for high temperature (10).The pressure required to ensure the seal is made possible by threadspresented on pins and nuts placed on the guides.

The called central cylinder region (R2), shown in FIG. 1 corresponds tothe main area of process control. The central cylinder preferably hasdiameter (D) of 3500 mm and height (H) of 4800 mm. Its lateral surfacehas a series of holes, shown schematically in FIG. 2, provided with flowcontrol mechanisms (11) (control valves). These valves are distributedas follows: four (4) columns of valves equally spaced along theperimeter of the cross section and each column there are valvesdistributed in 7 positions along the furnace height. There are a totalof 28 holes (11) through which they can inject gas into the furnace oruse as a leak in case of overpressure during the conversion of biomassinto charcoal. These 28 valves (11) are responsible for providingatmospheric oxygen to the perimeter area of the furnace. Furthermorethere were placed four (4) tubes which connect the furnace wall to itsinside in a diameter close to the center. These four tubes are alsoequipped with flow control mechanisms. These mechanisms are ball valves,with ball in stainless steel and focus in material for temperature to150° C. With respect to height, the tubes are positioned at anintermediate height of the holes located on the lateral wall, with twotubes per level.

The height of each of the valves is determined according to the study ofthe furnace temperature profile. In this study, it was evaluated thespeed when the temperature isotherm at 200° C. value moves along thefurnace height. The value of 200° C. is said by studies in the area asthe temperature at which finishes the drying of wood, i.e., from thistemperature begins to roast, followed by carbonization process itself.The studies developed for the preparation of the proposed solutiondemonstrated that the step of greater length of the conversion processis the drying of the wood linking water, we sought to study the isothermbehavior at 200° C. in the furnace and the means to promote theacceleration of its movement, thus accelerating the drying process. So,it was proceed with analysis of the isotherm velocity displacement at200° C. due to the positioning of the holes. The data obtained fromlaboratory tests have shown that the speed with which this isothermadvances in the furnace bed is reduced gradually from the furnaceignition point forward. Only there is the increase in speed ofpropagation when new approach occurs from an oxygen entry point. Giventhe typical behavior of the speed of isotherm with value of 200° C., itwas possible to affirm and optimize what would be the recommendedminimum distances between atmospheric gas inlet holes. The positioningof the holes along the height of the central cylinder region to itsoptimum configuration can be seen schematically in FIG. 1, according tothe detailed study should be distributed as follows: four holes with a2″ diameter in the position (H1) between 5% and 7% of the total heightof the cylindrical region measured from the base of the centralcylinder, 4 holes with a diameter of 2″ at the position (H2) between 18%and 26% of the total height of the cylindrical region measured from thebase of the central cylinder, 4 holes with a diameter of 2″ at theposition (H3) between 30% and 38% of the total height of the cylindricalregion measured from the base of the central cylinder, 4 holes with adiameter of 2″ at the position (H4) between 60% and 54% of the totalheight of the cylindrical region measured from the base of the centralcylinder, 4 holes with a diameter of 2″ at the position (H5) between 62%and 68% of the total height of the cylindrical region measured from thebase of the central cylinder, 4 holes with a diameter of 2″ in position(H6) between 78% and 84% of the total height of the cylindrical regionmeasured from the base of the central cylinder, four holes with a 2″diameter in the position (H7) between 94% and 98% of the total height ofthe cylindrical region measured from the base of the central cylinder;all holes are equipped with valves for flow control. The minimumdistance between tubes positioned between the holes on the cylinder sideis 26% of the total height of the cylindrical region measured from thebase of the central cylinder, it is recommended the use of these tubesbetween the levels located in the furnace base, because at this part theconducting of carbonization process becomes more critical.

In FIG. 2, close to each of holes and tubes, one sensor monitors thetemperature at the side (12) and inside the furnace (12 a ) with the aimof providing an accurate indication about the status or progress of theprocess carbonization and ensure that the safety limits for properfurnace operation are not exceeded. These devices for measuringtemperature may be K-type thermocouples that are embedded in thermowellswhich house the sensor and electrical connections of tar vapors andmists present inside the furnace. For purposes of control, beyond theside thermocouples, a series of temperature sensors is installed insidethe furnace (12 a ) near the central region, for a better monitoring ofthe procedure.

The region of the central cylinder (R2) is internally coated withseveral layers of materials which thermally insulate the metallichousing. The industrial furnace for charcoal production works withprocess temperatures of around 400° C., but in the region of the holesthis temperature can reach peaks of up to 1100° C. This occurs due tothe entry of external atmosphere oxygen from the interior furnace, whichin contact with the fuel gas and ignition source form a flame like ablow torch. Technically there are materials on the market that canwithstand the high temperatures described in this report, but thecarbonization process has aggravations that makes impossible theisolated use of these materials. During carbonization are released inaddition to the condensable and non-condensable gases, water vapor, tar,pyrolignous extract and volatile compounds present in the ash. The tarinside the furnace is in the form of a fine mist, which would pervadeand damage certain types of insulating blankets, as well as the alkalispresent in the ash. Furthermore, most of the refractory materialpresents a percentage of total passageway pore, i.e., they are poresthat connect hot face to the cold face allowing the passage of tar,which could damage the outer wall of the furnace. Both the tar, aspyrolignous extract have in their composition a portion of acetic acidwhich reflect the corrosive nature of the internal atmosphere. Somerefractories are incompatible with acidic atmospheres or water vapor.The material to be loaded by the top of the furnace reaches the innerwalls with impact, causing wear by abrasion and break conventionalrefractory materials. The invention, object of this report proposes asolution so as to thermally insulate the furnace, ensuring temperaturein the housing of the order of 100° C. and reducing in the maximum thetar passage to the outer wall. The proposed solution is a combination ofmaterials that alone could not meet the process needs, but together meetwith accuracy and efficiency. For the region of the holes (considered inthis report, the region comprised in a radius of between 100 mm and 200mm taken from the hole center), the materials for promoting theisolation of internal surface of the metallic cylinder to the insidefurnace are ceramic fiber blanket (13) with 2-inch thick, insulatingmaterial of low density and relatively low cost (this material is themain responsible for the reduction of the temperature in the furnacehousing); smooth stainless steel plate of 1.5 mm thickness (14) coveringthe entire exposed surface of the blanket; refractory low cementconcrete with at least 45% of Al2O3 mixed with metal fibers in stainlesssteel at a proportion of 2% by mass of concrete (15) used—this concreteassociated with the use of metallic fibers ensures integrity coconcrete, avoiding the spread cracks due to process temperaturevariation. For the outside region of the holes and ignition points, therefractory concrete with metallic fibers is substituted by a refractoryconcrete with at least 47% of Al2O3 and maximum density of 2.27 kg/m3applied on a hexagonal mesh, suitable for concrete anchoragerefractories, with total thickness of 27 mm. The use of this concrete inthis region coupled to a special curing process reduces the totalpercentage of full bore pores to 5%.

In FIG. 1, the area called the lower frustum (R3) consists of aninverted frustum, or in a transition of a circular cross-section to asquare with rounded corners made of sheet metal. In FIG. 2, this cone(16) must be drilled to allow the passage of gases from biomass bed tothe bottom, however, retaining the biomass. It is recommended that theholes have a diameter of 40 mm with an average spacing of 120 mm holes,or at least 20% of free passage area in the lateral area of the cone.The tilt angle for the cone should be such that promote the flow ofcharcoal without retentions flow. FIG. 1 shows for charcoal this angle(A2) varies between 30° and 50°, with an optimum configuration theinclination of 36°. The larger diameter of the frustum must follow thediameter of the central cylinder region.

Located in the lower portion of the lower frustoconical region and seenin FIG. 2, it is located a discharge valve (17) of charcoal. This valveconsists of a blocking surface of the solid material located above itand must allow the passage of gas and condensables generated in theprocess. The valve must be mobile, clearing the passage at the end ofthe carbonization process in order to unload the charcoal produced. Forthat meets the minimum requirements, this valve must be flat with holesdistributed over the surface uniformly so as to allow the passage ofgases and retaining solid objects such as the inverted frustum. Thediameter of the holes may be similar to that used in the cone, but thepercentage of hollow area on the opening area must be at least 20% inorder to ensure maximum flow for the gas flow. A flat surface with ahole (18) is installed on a frame provided with wheels (19), which inturn is on a track that allows the displacement of the cap and structurein only one direction. Turning the structure to the external environmentthere is a stainless steel metal rod (20). The set cover, frame withwheels and rod gives the name of car cover. In the lower region, some ofthe frustum holes (21) establish, through ducts, contact with theexternal environment for the injection of gases, such as atmosphericair, dosed for specific control mechanisms such as valves. These valvesare ball valves, with ball in stainless steel and seat in material fortemperature up to 150° C. The cover may be made of special steel alloysuch as ASTM 572.

In FIG. 1, the total height of the volume (HC) comprised by the threeregions (top (R1), core (R2) and lower frustum (R3)) on the diameter (D)of the central area (central cylinder) should vary between 1.0 and 2.2.The range of the central cylinder diameters ranges from 3300 mm and 4580mm, recommended value as optimal configuration of the furnace.

The internal volume of the furnace, available to receive the biomass asfeedstock, consisting of the three regions (top (R1) central cylinder(R2) and lower frustum (R3)), hereinafter called “conversion zone “mayhave volumetric capacity between 35 and 65 m3 with satisfactory results,and the optimum condition equal to 50 m3.

The conversion zone is maintained upright by a holding device whoseshape is the association of a frustum and a cylinder with definedproportions made of sheet metal. This device consist of a fundamentalpoint for the invention as will be shown below. This support structureshown in FIG. 2, also called “furnace skirt” (22) acts as an expansionbox in the process, allowing the accumulated gases in the furnace baseto recirculate, providing an atmosphere of hot gases and facilitatingthe conduction of process for the preheating of the biomass at thebottom of the furnace. In case of overpressure in the lower frustumregion, the “furnace skirt” (22) is provided with specific pressurerelief devices, called relief valves (23). Such relief valves mustalways be symmetrically distributed, and along the circumference of thefurnace. The relief cap should be compatible with the area and weight ofthe furnace, raw material and process for this invention thatcorresponds to an area ranging between 0.25 and 0.6 m2 and weighingbetween 90 and 160 kg. Its position is limited to the lateral area ofthe frustum truncated cone and should be equipped with a duct or chimney(24) that directs the flow from the pressure increase in process or in asecure location. The smaller diameter of the support structure is equalto the diameter of the central cylinder region, with the point of unionbetween the “furnace skirt ” (22) and the central cylinder (R2) of about200 mm above the lower limit. The higher diameter (DB) may vary between1.25 to 1.35 times the diameter of the central cylinder region. Thestructure is coated internally with ceramic fiber blanket (25) with adensity of 128 kg/m3, protected by a stainless steel flat plate (26)with 2 mm thick. The skirt also acts as an equalizer of the center ofgravity of the furnace to make its operation safer about the possibilityof an imbalance and toppling.

The furnace support base of the supporting structure of the furnace isprovided with water channel (27) for cooling of the carbonization systemcoupling sealing. Next to the furnace support base are present guidesfor coupling the furnace to the support base of the carbonizationsystem.

The invention, object of this specification, is provided with specialholes called ignition points of process (28). These points may belocated in the three regions of the conversion zone, however the idealposition for the ignition process is lower region of the centralcylinder shown in FIG. 1, the position (HO) between 5% and 15% of thetotal height of cylindrical region measured from the base of the centralcylinder. The location of this point in the limit given above allows abetter control of the process, since although the isotherm of 200° C.gradually advance the ignition point for the rest of the furnace, theignition in this height of the furnace allows that by means of the hotgases of the ignition process occurs a preheating of the entireconversion zone, increasing the isotherm velocity of 200° C. The sizefor the hole destined for the ignition process can vary between 4 and 6inches. Similarly to the holes for the entry of atmospheric air, theignition holes must be equipped with air flow control devices. As basicrequirements for operation the guarantee of sealing, the hole areashould not have obstructions (such as, for example, butterfly typevalves whose outflow obstruction element bisects the flow passage area)and should be resistant to temperatures up to 200° C. Therefore, it isrecommended the use of ball valve, with stainless steel ball and seatmaterial for temperatures up to 200° C. Due to the high temperaturesnear the ignition point, it is installed in this region a refractoryblock with at least 70% of A₂0₃, resistant to temperature of 1600° C.

In addition to the furnace described above, this invention makesexclusive use of the carbonization system described below and shown inFIG. 3.

The carbonization system, integrant part of the industrial furnace forthe production of charcoal, comprises a movable support base (29),condensable recovery equipment (30), safety device for pressure relief(31), exhauster (32) and conducting ducts of gases and vapors (33). Thecarbonization system is a fixed equipment in a carbonization plant andthe furnace is a movable device that couples to this system.

The movable support base is constituted by a cylindrical ring (34) ofdiameter equal to the largest diameter of the supporting structure,built of metallic material. Attached to the ring are the guides (35)which has the function of assisting the furnace positioning on themovable support base. Also on the movable support base are installedpivot pins (36) that fit on the guides of the furnace support base (37).Through this mechanism, with the aid of a system of nuts and spindles,the furnace is kept pressed against the movable support base. The seal(38) between the furnace and the movable support base is promoted by theuse of special rubber for temperatures up to 90° C. Internally connectedto the support ring, an inverted truncated cone (39), made of steelplate, allows uniform capture of the entire gaseous stream andcondensable. The larger diameter of the cone should accompany the minordiameter of the supporting ring. The opening angle (A3) should bebetween 40° and 60° and the smaller diameter (DC) should be sufficientso that the gas flow speed does not exceed 10 m/s.

The movable support base receives this name for being allocated on anindustrial weighing system, with articulated loading cells (40)(typically used for road scales) to absorb any lateral shift caused bycollision between the furnace and the guides (35) and between thefurnace and the movable support base. Therefore, the base has freedom tomove vertically, allowing the correct weighing of the material.

Connecting the movable base support to the exhauster, there are a numberof pipelines and equipment that conduct the gases and condensable fluxout of the furnace. These gases and condensable can be used in otherprocesses, such as combustion to supply heat energy, among others. Dueto the presence of the weighing system, the connection between thesmaller diameter of the inverted cone movable support base and the firstsection of the gas pipe must be made using a flexible junction (41).This junction (41) must be resistant to temperatures up to 265° C., madeof stainless material and free of spaces where condensable material canaccumulate and impair the flexibility of the joint. The solutionpresented in this invention is the use of two concentric pipes, beingthe smaller diameter tube (42) physically connected to the invertedtruncated cone (39) of the movable support base and the largest diametertube (43) connected to the expansion box (44). To prevent false airbeing sucked through the gap between the pipes, a flexible junction (41)made of glass fiber fabric coated with a plastic film, involves theducts. This flexible junction (41) having one end attached by clamps tothe cone (39) in the upper position and the other end attached to thelarger tube (43) at the bottom. This assembly allows perfect operationof the weighing system, since it disconnects the set that is supportedon the loading cells from the rest of the equipment. Is avoided, thus,the possibility of creating a “lever effect”, when the weight of thefuel/carbon contained in the furnace would be influenced or sufferchanges depending on the gas flow and pipe handling and remainingsystem, which would be connected the cone.

Attached to the larger duct, used to connect the expansion junction tothe movable support base, there is an expansion box (44) for reducingthe flow rate and deposition of particulate matter and condensable. Thespeed in this region will be reduced to 50% of the speed in the duct.The expansion box is provided with two flow outputs. The first islocated on the base of the box and is provided with a filter (45) whichallows only the flow of condensable to a storage tank (46). The secondoutput located on the box lateral of the expansion box allows output ofgases, vapor and mist still dispersed in the gas stream. In this secondoutput, the duct (33) is dimensioned not to have flow velocity exceeding16 m/s. This duct follows leading the gases to the exhauster.

At the end of the duct (33), the connection to the exhauster is madeperpendicular to the length of the pipe. This is because an explosiondoor (47) is installed at the end of the duct to ensure operationalsafety and integrity of the equipment in case of overpressure in the gaslines and/or return of the flame resulting from the flaring of gas inthe incinerator. The explosion door is composed of a flat surface, whichis kept closed by using only the own weight of the cover. In case ofincreased internal pressure, the door opens, relieving the internalpressure and directing, through a chimney (48), the exhaust flow to asafe region. This region or gas receiving location should preferably besuitable for burning the gas with capacity for complete combustionthereof.

The exhauster (32), one of the major component of the process, consistsof a centrifugal exhauster with nominal flow of 10.000 m³/h and staticpressure of at least 250 mmca. The rotor must be made of stainlesssteel. The equipment must be equipped with speed controller to allowadaptation thereof to the use of different forms of biomass andproduction process.

The industrial furnace for the production of charcoal has a device forrapid unloading of coal still warm in order to release the furnace forthe carbonization process as soon as possible. FIG. 3 shows this device.

The basis for unloading comprises a platform that has a truncated cone(49) with the largest diameter compatible with the largest diameter ofthe bearing structure (DB) and smaller diameter compatible with thedischarge valve (17). Below the platform there is a movable cylindricalcontainer (50) with capacity between 24 and 32 m³ of charcoal. Themovable cylinder has 3 to 5 water spray nozzles (51) with a flow rateranging between 5 and 20 L/min, which are positioned in its interior tocool the burning coal during and after unloading.

On the procedure for operating the furnaces.

The industrial furnace for production of charcoal is loaded with biomassby the upper opening in the in the central cylinder region. For theloading, due to high volumetric capacity of these furnaces, it ispreferably recommended the use f conveyor belt with or without silos orstorage cylinders/stock, to ensure the constant supply of biomass to thefurnace. This procedure ensures a quick loading time, which preferablyshould be less than 5 minutes to the feeding of 50 m³ of splinter in thefurnace whose internal temperature must be above 200° C.

Then the top cover or top region is placed on the central region of thecylinder and fastened thereto with the aid of the threaded pivot pins,guides and nuts. The carbonization furnace is then moved to thecarbonization system, where it is then positioned and locked on themovable support base.

Once the furnace is locked, the exhauster is turned on and adjusted sothat its speed be compatible with the material used. Typically, it isaimed the maintenance of a constant volumetric flow rate of 6.000 m³/h,being the rotation speed adjusted so that the aforementioned flow ratebe obtained.

The ignition process is then initiated. First it is assured that thevalves located at the top of the furnace are opened to create acontinuous flow of gases within the furnace. Only then the ignitionitself takes place. Through the 4 ignition points of the process, asmall amount not exceeding 2 kg of needles or burning coal, is injectedinto the furnace. The heat generated in these 4 points propagates by thelower region while a hot gas stream rises through the bed heating it.The strategic position of the ignition point allows the preheating to atemperature higher than 200° C. all the volume of the bed, optimizingthe process, since with all the furnace above 200° C. the conduction ofthe carbonization becomes faster.

The carbonization process is then controlled by the air inlet holes,which are opened to permit entry of oxygen, which in turn leads topartial combustion of gases inside the furnace. This burning suppliesenergy to the rest of the endothermic phase of the carbonizationprocess, being in the sequence closed the holes whose regions havereached the limit temperatures for the process.

This process of opening and closing of the valves is repeated until allof the internal volume is at temperatures above 350° C. Throughout allthe period the furnace has its weight and temperature continuouslymonitored. The end of the process is reached when the weight of thefurnace charge is equal to the weight stipulated as production targetfor the furnace.

When production target is reached, the furnace is then uncoupled andremoved from the support base and the exhauster is turned off. Thefurnace is then positioned on the unloading basis wherein automaticunloading mechanisms connected to cover car rods unblock the orifice ofthe bottom cone region for the unloading of burning coal, withtemperatures above 300° C. During the drop of the burning coal, waterspray nozzles directed to the descending coal flow promote a superficialcooling of coal. The discharged coal is accumulated in a specialcontainer, metallic, non-insulated, for the cooling. Once completed theunloading process, which preferably does not exceed 3 minutes, thevessel containing hot charcoal is closed and sealed, from which followsto complete its cooling process.

The cooling process takes place by natural convection and the enthalpiceffect of the removal of evaporation heat of the water that is sprayed,strategically in the regions of the carbon bed where the temperatureexceeds 120° C.

This process step, which lasts 10 to 15 hours, ensures the release ofthe container furnace for continuous charging process, carbonization,unloading, loading, carbonization, unloading . . . and so on in cycleslasting between 3 and 6 hours.

The container furnace tested in pilot scale laboratory had its designoptimized, resulting in the manufacture of a pilot furnace on anindustrial scale. The changed items were especially related to increasedwood put into the furnace capacity, improved instrumentation, control,mechanization, operating procedure, process and thermal size. In thisfurnace the parameters monitored during the running are: load weight,flow rate, composition, density, pressure and gas temperature, air inletflow in load, temperature of sampled firewood in more than 70 pointsaround the furnace volume and volume of pyrolignous generated.

All data was generated continuously in real time and simultaneously. Thetests have converged to a stabilized process under the followingconditions: volumetric yield of 1.3 st of wood for per m³ of charcoal,gravimetric yield of 35%, carbonization time of 3 h, generation of 6.500m³/h per furnace with an average PCI of 1.700 kJ/m³, possibility ofthermal power generation from furnace of 3 MW or equivalent togenerating 1 MWe per 1000 tons of coal, producing 150 liters ofpyroligneous per cycle, charcoal production with 200 kg/m³ bulk density.These results demonstrate that the industrial Container furnace ofcharcoal production, or Furnace Container Rima (FCR) consists of apioneer industrial technology in charcoal cogeneration and thermal powercapable of generating electricity technically and economically viableway.

-   -   The development of this project enabled the mass and energy        balance detailing in the FCR, whose values show that in this        furnace there is excess of oxygen; the combustion occurs with        all products derived from the process (gas, tar, pyroligneous        and coal). And in addition to the combustion reaction, it was        verified that occur important intermediate reactions, such as        carbon exothermic reaction with water vapor, gasification and        cracking. These intermediate reactions which occur in the        furnace, with an operational exclusivity that is being requested        in this application, are responsible for an innovative result in        the state of the art of carbonization technology. That is, only        in the structural, operational, thermal and mechanical        conditions of this project, it is possible to produce coal with        a gravimetric yield of 35% while a gravimetric yield of 60% gas        is obtained, against traditional values, around 30% for the        generation of gas. This means that the furnace has a very        significant difference from current carbonization furnaces: the        generation or preferential production of gas relative to tar and        pyroligneous (the condensable fraction ends up gasifying). This        is an essential factor to promote the association of this        carbonization project to a Thermoelectric central with        simultaneous burning of biomass and gas carbonization. With a        fraction of condensable contained in the generated gas        transport, displacement, storage and piping become feasible to        be conducted to a plenum or a balloon, where it is homogenized,        and then to direct combustion in a boiler in order to promote        the generation of electricity.        -   i. The mass and energy balance, resulted in the verification            of a highly efficient process. The thermal losses are            inferior to 5%. The energy percentage available necessary to            maintain or sustain the pyrolysis is 10%. The energy            contained in the coal around 60% of the energy present in            the wood and in the gases of 25%.

APPLICATION EXAMPLES

Below, it will be shown a series of possible configurations for theinvention, which aim illustrate its several uses. And, although it canbe exemplified by, it is not limited to the examples that follow.

Example 1

The industrial furnace of production of charcoal with capacity for 35 m3can be loaded by the upper hole with wood cavacos, average granulometrybetween 100 and 120 mm. The furnace, already with the cover placed andlocked, is placed on the carbonization system and locked on the movablesupport base. The exhauster is then switched on and the ignition onspecific points, with ember, starts. The carbonization control by theopening and closing of the holes follows in order to provide energy forthe endothermic phase. The process ends in about 3 hours, producing 2400kg of charcoal with gravimetric yield of 33%.

Example 2

The industrial furnace for charcoal production with a capacity of 35 m3can be loaded by the upper hole with wood small logs, average size of200 mm. The furnace already with the cover placed and locked, is placedon the carbonization system and locked on the movable support base. Theexhauster is then switched on and the ignition on specific points, withember, starts. The carbonization control by the opening and closing ofthe orifices follows in order to provide energy for the endothermicphase. The process ends in about 5 hours, producing 2800 kg of charcoalwith gravimetric yield of 35%.

While illustrative embodiments have been illustrated and described, itwill be appreciated that various changes can be made therein withoutdeparting from the spirit and scope of the invention.

1. Industrial process using metallic furnace with forced exhaust andmechanisms developed for concomitant production of coal, fuel gas,pyroligneous extract and tar, characterized by simultaneously operatingwith other batteries of furnaces, preferably, 6 carbonization platforms,allowing a monthly production of more than 20,000 m³ of charcoal andmore than 10.000 m³/h of fuel gas with calorific value higher than 1500kJ/m³.
 2. Industrial process using metallic furnace with forced exhaustand mechanisms developed for concomitant production of coal, fuel gas,pyroligneous extract and tar, according to claim 1, characterized forbeing part of a chemical plant, with simultaneous production ofcharcoal, tar, pyroligneous and fuel gas.
 3. Industrial process usingmetallic furnace with forced exhaust and mechanisms developed forconcomitant production of coal, fuel gas, pyroligneous extract and tar,according to claim 1, characterized by presenting a potential ofelectric power generation of up to 1 MWe to each 1000 tons of coalproduced per month.
 4. Industrial process using metallic furnace withforced exhaust and mechanisms developed for concomitant production ofcoal, fuel gas, pyroligneous extract and tar, according to claim 1,characterized by presenting a thermal loss less than 5% of the initialenergy contained in the wood, with 25% of humidity, a gravimetric yieldhigher in coal above 33% and a gravimetric yield in fuel gas higher than60%.
 5. Industrial process using metallic furnace with forced exhaustand mechanisms developed for concomitant production of coal, fuel gas,pyroligneous extract and tar, according to claim 1, characterized bypresenting a percentage of the available energy, required to maintainand sustain the pyrolysis of 10% of the original energy contained in thewood, with humidity around 25%.
 6. Industrial process using metallicfurnace with forced exhaust and mechanisms developed for concomitantproduction of coal, fuel gas, pyroligneous extract and tar, according toclaim 1, characterized by allowing automation of the process from theopening of the valves, as continuous monitoring and online of the totalweight, volumetric thermal profile and characteristics of the gas flow:composition and flow.
 7. Industrial process using metallic furnace withforced exhaust and mechanisms developed for concomitant production ofcoal, fuel gas, pyroligneous extract and tar, according to claim 1,characterized by allowing direct burning of the fuel gas generatedduring carbonization, being unnecessary a pre-treatment of gas, infunction of the gas does not exhibit harmful components and/orcomponents which may damage the operation of a steam boiler. 8.Industrial process using metallic furnace with forced exhaust andmechanisms developed for concomitant production of coal, fuel gas,pyroligneous extract and tar, according to claim 1, characterized byallowing the simultaneous burning of fuel gas generated in thecarbonization with biomass in a boiler, whose steam generated can reachpressures above 40 bar and in this condition turn a turbine to generateelectricity.
 9. Industrial process using metallic furnace with forcedexhaust and mechanisms developed for concomitant production of coal,fuel gas, pyroligneous extract and tar, according to claim 1,characterized by allowing the burning of the fuel gas generated in thecarbonization in preferably one or more entries of the boiler, thisentry, positioned on the biomass burning rotated-grid in order tominimize the need for secondary air entrance in the boiler. 10.Industrial process using metallic furnace with forced exhaust andmechanisms developed for concomitant production of coal, fuel gas,pyroligneous extract and tar, according to claim 1, characterized byallowing in a unique and innovative way the recovery of the energycontained in the forest in its most noble form: production ofsustainable solid fuel and electric power generation, with exclusiveburning of biomass and gas from carbonization, avoiding the need for tarand pyroligneous recovery, which are turned into gas during the process.